KR830002053B1 - Air elutriation device for recovering char fines in discharge waste from iron oxido reclucing kiln - Google Patents

Air elutriation device for recovering char fines in discharge waste from iron oxido reclucing kiln Download PDF

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Publication number
KR830002053B1
KR830002053B1 KR1019810003082A KR810003082A KR830002053B1 KR 830002053 B1 KR830002053 B1 KR 830002053B1 KR 1019810003082 A KR1019810003082 A KR 1019810003082A KR 810003082 A KR810003082 A KR 810003082A KR 830002053 B1 KR830002053 B1 KR 830002053B1
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KR
South Korea
Prior art keywords
particles
air stream
air
fine
kiln
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Application number
KR1019810003082A
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Korean (ko)
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KR830005910A (en
Inventor
웨슨 긋델 토마스
Original Assignee
제프리 엔 보울러
더 디렉트 리덕션 코오포레이션
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Priority to US06/180,941 priority Critical patent/US4299694A/en
Priority to US180941 priority
Application filed by 제프리 엔 보울러, 더 디렉트 리덕션 코오포레이션 filed Critical 제프리 엔 보울러
Publication of KR830005910A publication Critical patent/KR830005910A/en
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Publication of KR830002053B1 publication Critical patent/KR830002053B1/en

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    • BPERFORMING OPERATIONS; TRANSPORTING
    • B07SEPARATING SOLIDS FROM SOLIDS; SORTING
    • B07BSEPERATING SOLIDS FROM SOLIDS BY SIEVING, SCREENING, OR SIFTING OR BY USING GAS CURRENTS; OTHER SEPARATING BY DRY METHODS APPLICABLE TO BULK MATERIAL, e.g. LOOSE ARTICLES FIT TO BE HANDLED LIKE BULK MATERIAL
    • B07B11/00Arrangement of accessories in apparatus for separating solids from solids using gas currents
    • B07B11/04Control arrangements
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B07SEPARATING SOLIDS FROM SOLIDS; SORTING
    • B07BSEPERATING SOLIDS FROM SOLIDS BY SIEVING, SCREENING, OR SIFTING OR BY USING GAS CURRENTS; OTHER SEPARATING BY DRY METHODS APPLICABLE TO BULK MATERIAL, e.g. LOOSE ARTICLES FIT TO BE HANDLED LIKE BULK MATERIAL
    • B07B11/00Arrangement of accessories in apparatus for separating solids from solids using gas currents
    • B07B11/06Feeding or discharging arrangements
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B07SEPARATING SOLIDS FROM SOLIDS; SORTING
    • B07BSEPERATING SOLIDS FROM SOLIDS BY SIEVING, SCREENING, OR SIFTING OR BY USING GAS CURRENTS; OTHER SEPARATING BY DRY METHODS APPLICABLE TO BULK MATERIAL, e.g. LOOSE ARTICLES FIT TO BE HANDLED LIKE BULK MATERIAL
    • B07B4/00Separating solids from solids by subjecting their mixture to gas currents
    • B07B4/02Separating solids from solids by subjecting their mixture to gas currents while the mixtures fall
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B07SEPARATING SOLIDS FROM SOLIDS; SORTING
    • B07BSEPERATING SOLIDS FROM SOLIDS BY SIEVING, SCREENING, OR SIFTING OR BY USING GAS CURRENTS; OTHER SEPARATING BY DRY METHODS APPLICABLE TO BULK MATERIAL, e.g. LOOSE ARTICLES FIT TO BE HANDLED LIKE BULK MATERIAL
    • B07B9/00Combinations of apparatus for screening or sifting or for separating solids from solids using gas currents; General arrangement of plant, e.g. flow sheets
    • B07B9/02Combinations of similar or different apparatus for separating solids from solids using gas currents
    • CCHEMISTRY; METALLURGY
    • C21METALLURGY OF IRON
    • C21BMANUFACTURE OF IRON OR STEEL
    • C21B13/00Making spongy iron or liquid steel, by direct processes
    • C21B13/08Making spongy iron or liquid steel, by direct processes in rotary furnaces
    • Y02P10/136

Abstract

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Description

Air scrubbing method for recovery of fine carbide particles in exhaust waste from iron oxide reduction

1 is a schematic diagram of a system including a lightening device for implementing the method of the present invention.

2 is a side view of the device of FIG.

3 is a perspective view of a hopper / spreader disposed in the feed slot shown in FIG.

FIELD OF THE INVENTION The present invention relates to particle separation, ie, elutriation techniques, and more particularly to a process for directly reducing iron oxide in rotary kilns using solid carbonaceous reducing agents as fuels and reducing agents. The present invention relates to a method for separating fine carbide particles from waste discharges.

Emissions from the rotary kiln that directly reduce iron oxides and other oxide-containing materials using solid carbonaceous materials such as coal as fuel and reducing agent are magnetized after screening, so that sponge iron or metal Attached to a magnet, it is removed from its emissions and only the non-magnetic portion of the emissions, including carbonized coal and fines, is passed through and separated. Large pieces of carbonized coal and carbide are recycled to the rotary kiln and only fine carbides are contained in the final waste. The fine carbide sent to the waste is a significant amount of loss in the process and additional coal must be supplied to the kiln in a timely manner proportional to the carbides entering the waste in the process. Particularly in recent improvements to the operation of this type of direct reduction process, as described in the applicant's U.S. Patent Application No. 132,806, the loss of fine carbides is of great importance, which is combined with coal through the exhaust end of the kiln. Or by feeding it without coal, the carbides can be effectively recycled.

To enhance the efficiency of this type of process and related processes, the present invention is used in a product separation system to recover light particles such as microcarbide from heavy waste particles, thereby recovering and recycling the carbides at high percentages of recovery and requiring them in the process. It can reduce the amount of new coal that is produced.

According to the present invention, there is provided a system comprising an air scrubber that is particularly suitable for use in classifying and separating components in emissions from coal combustion processes containing partially combusted, specialized particles of coal. The dishwashing device consists of a housing having a chamber in which the discharge is uniformly injected from a hopper spreader. The discharge receives a backflow air stream generated by the discharge device connected to the top of the chamber. Light particles of carbonized coal or carbide are moved upwards by their airflow, and relatively heavy particles of metal such as DRI, refractory pieces, desulfurizers and other treatment agents fall downwards in the chamber. The lower part of the chamber is provided with a series of transversely arranged separation rods, the separation rods of which are adjustable in their relative placement directions to enhance the separation and desired flow of air flow to enhance the separation action. Provide separation rate. The bottom of the housing is open and dimensioned to allow air to flow at approximately half the separation rate. Additional air may be injected in the upper portion of the chamber to assist in transporting light, ie low density, particles suspended upwards into a low efficiency cyclone for collection. Heavy particles, on the other hand, may fall through the lower open end into the hopper and be sent to a magnetic separator for continuous sorting or for continuous separation and processing.

The invention is explained in more detail below with reference to the accompanying drawings.

A system comprising a distillation apparatus 1 for carrying out the method according to the invention is shown in FIG. 1, which system is particularly useful for separating particles of various types in a relatively fine portion of the emissions from a coal combustion process. . In many coal-fired processes, partial combustion particles of coal are found in the emissions and therefore have to be separated off, after which they can be recycled to the process or sent to waste. In the process for the direct reduction of ore and other materials containing iron oxides in the rotary kiln, for example using solid carbonaceous reducing agents as fuel and reducing agent, the material exiting the kiln is screened and then magnetically separated. Sponge iron or DRI products and coarse carbides are separated and recovered, and the remaining fine particles are usually sent to the waste. The particles may include carbide particles, fine ash, fine sponge iron, refractory pieces, iron oxides, sulfur regulators, inert wastes, and the like. Large carbide particles separated and recovered from the DRI are recycled into the process. However, conventionally, many fine carbides are contained in the waste because they mix with other fine particles that form contaminants when they are returned to the process. Of course, the greater the percentage of carbide that can be recycled, the more efficient the process is, because less coal is used in the overall process. Dimmer 1 provides a simple and efficient method and means for separating fine carbides from fine waste using air filtration to classify particles based on their density and their aerodynamic properties.

As can be seen in FIG. 1 the light device 1 has a housing which can be in the form of a rectangular box-like structure 2 with a hollow interior forming a chamber 2a. Air flows upwards (as indicated by the straight arrows) by the exhaust system through chamber 2a. The exhaust system consists of an exhaust device 10 having an exhaust fan and 11 air conditioning fans 12, the exhaust device being connected to the collector cyclone 20 by an exhaust pipe 13, the cyclone 20 being connected by a pressure tube 21. It is connected to the top of the light device 1. The top of the dishwasher consists of a lid, the pressure tube 21 is connected to the lid, and the lid 3 is hermetically mounted on the top of the box-like structure 2. The lid 3 is also provided with holes 3a, which are fitted with a bleed damper 4 which regulates the injection of air into the upper part of the chamber 2a.

A feed slot 5 is formed in the center of the box-like structure 2 through which material to be sorted is injected into chamber 2a.

In this region of chamber 2a, most of the components of the material are separated. Air is injected into the chamber 2a at the open lower end of the chamber 2a between the lower perimeter 2b of the box-like structure 2 and the collecting trough or hopper 30a of the hopper 30 disposed below the chamber 2a. The cross-sectional area of the base of the box-shaped structure 2 with respect to the area formed by the upper periphery 30a of the homper 30 is given by the air inflow rate into the chamber 2a. The rate of air in the central part of the chamber where the separation takes place should be such that the rate of separation of the material introduced through feed slot 5 into the separation zone is not exceeded. That is, the air inflow rate is preferably half the separation rate, so that the area formed by 30a of the upper peripheral portion of the hopper 30 is about twice the cross-sectional area of the box-shaped structure.

In the area between the separation zone and the open lower end of box-like structure 2, a series of separator rods 40 are arranged across chamber 2a to control the separation rate and the flow of air passing through. As shown in FIG. 2, slots 50 are formed in the shaft portions of the box-shaped structure 2 so that the upper and lower rods 40a and 40b can be disposed on the upper side. This arrangement can be used to obtain the proper separation rate and alternating current. This is because the close arrangement of the rods reduces the cross-sectional area passing between them, increasing air velocity and alternating action in the vicinity. The central rod 40c can be moved horizontally back and forth within the slot 51 between the fixed rods 40d to equalize the air flow and enhance the separation action for particles in the separation zone, which is the width of one side of separator structure 2 This is because the primary supply is performed at one side through the supply slot 5 formed over.

Feed slot 5 is equipped with a cracker structure 60 shown in FIG. 2, into which the fine particles to be separated are screened and separated from the main effluent from a suitable coal fired process. The distributor structure 60 is in the form of a hopper with the spreader 70 shown in detail in FIG. The spreader 70 may be of a conventional type consisting of an elongated trough 71 formed at the bottom with a series of holes in the form of holes or slots for the passage of particles. The slots are preferably formed in a fan-shaped range of about 45 ° with respect to the center of curvature at the bottom of the trough, and the size of their openings is controlled by the adjustable cover plate 76.

A distributor vane 73 whose shaft is arranged along the bottom grain center of the trough 71 is rotatably installed in the trough by a suitable drive motor 77 (FIG. 2). The splitter vane 73 has four arms 74, which have curved serrated edges 75 formed thereon, which, when the vane 73 rotates, explode and meter the particles fed into the trough 71 through the trough slot 72. Injection is uniformly through feed slot 5 into chamber 2a.

Separator structure 2 is provided with a transparent observation door 80 so that the internal state of the structure can be observed, and the structure 2 may be adapted to be supplied through slots on both sides. Observation 80 The upper portion of Structure 2, as described above, is in the form of exhaust lid 3, which lid 3 is the top of the lid and the particles contained in the air that are swelling upward into the exhaust pipe connected between the collector cyclone 20. Outer bore 3a may be provided for the bolted damper 4 to inject additional air into the chamber 2a to preserve the transfer. A suitable gauge 38 may be installed to measure the air pressure in lid 3.

For example, the operation of the light device 1 in separating light particles from fine emissions from a coal fired kiln is described below. In the first direct reduction process described above, the prescreened carbides, along with contaminants such as fine coal ash, refractory pieces, burnt limestone and fine DRI, are fed to distributor 60 installed on the side of separator 2 by a suitable conduit 90. All of the particles fall into the gap between the rotating distributor vane arms 74 and are broadly improved by the vanes 73 and are uniformly injected into the feed slot 5 of separator 2 through the openings in the bottom of the groove source 71.

After passing through feed slot 5 and being injected into chamber 2a, the particles receive a countercurrent air stream. Less dense and lighter particles are sucked upwards by the air stream and heavy and larger particles fall into the air stream. The aerodynamic resistance of the particles may tend to be incorporated within the separation action, but specific gravity controls the separation action because the surface of most particles is relatively small.

When the chamber is approximately 6 feet long and the sides are 1 and 2 feet wide, the airflow velocity above the rod 40 is approximately 13 feet per second, resulting in fine carbide particles, fine coal ash, refractory fragments, spent limestone, It has been found that good separation between the DRI and other fine particles can be achieved. Its air flow rate is the diameter

Figure kpo00001
The particles to be separated between the rods of inch
Figure kpo00002
In the inch range it may be changed between 10-18 feet per second by adjusting the exhaust damper 12. The internal pressure in the conduit 90 can be changed to an H 2 O negative in the range of about 0.1 to about 0.3 inches and is preferably maintained at about 0.2 inches H 2 O negative.

Heavy particles fall through the gap between the rods 40 and are injected into the collection hopper 30 disposed below chamber 2a. As mentioned above, the area formed by the upper periphery of the hopper should be about twice the area of the open bottom of separator 2. The particles collected in the hopper 30 can then be reclassified by a two stage decanter as needed to remove the fine carbide particles contained in the heavy particles. When used with the reduction process described above, the sorted particles containing fine DRI and non-magnetic fine waste are finally fed from the hopper 30 to the magnetic separator 35 and the fine DRI is recovered from the magnetic separator 35 and the non-magnetic particles are returned to the waste. Is sent.

The fine carbide particles transported upwards with the air stream are sent to the exhaust system via lid 3. The bulge damper 4 disposed in the hole 3a of the lid can be adjusted to inject additional air along the conduit 21 to the collector cyclone 20 to assist the transport. Cyclone 20 preferably has a low and variable efficiency such that only very fine particles, eg smaller than # 22, # 32, or # 42 mesh Taylor screens, pass through exhaust 10. The exhaust can be installed in a separate building to collect the particles in a suitable bag. Carbide particles can be collected at the bottom of cyclone 20 and discharged from the bottom through sealed valve 25 to be recycled to the main process or sent to another sorting stage in a similar separate scrubber with suitable controls. The flow of exhaust air is regulated in exhaust 10 by fan 11 along with damper valve 12. Dirt remaining in the exhaust air can be removed in a bag installed after the exhaust or in another suitable device.

The amount of coal required to feed the entire process by 20% by recovering and recirculating the fine carbide separated in the above-mentioned scourer and in particular by feeding the materials through the discharge end of the rotary kiln of the direct reduction process. Can be reduced.

Claims (1)

  1. A method for separating fine carbide particles from a mixture of microparticles in an exhaust from a direct reduction process during coal combustion, wherein the particle mixture is uniformly introduced into an upwardly flowing air stream and light carbide particles move upwardly with the air stream. And other heavy particles regulate the velocity flow of the air stream in the area of the air stream where the particle mixture is introduced to fall downward through the air stream by gravity and accommodate heavy particles falling downward in the hopper. And removing and collecting light carbide particles from the air stream by a low efficiency cyclone, wherein the fine carbide particles are recovered from the iron oxide reduction furnace.
KR1019810003082A 1980-08-25 1981-08-24 Air elutriation device for recovering char fines in discharge waste from iron oxido reclucing kiln KR830002053B1 (en)

Priority Applications (2)

Application Number Priority Date Filing Date Title
US06/180,941 US4299694A (en) 1980-08-25 1980-08-25 Method and apparatus for char separation from the discharge materials of an iron oxide reducing kiln
US180941 1980-08-25

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KR830005910A KR830005910A (en) 1983-09-14
KR830002053B1 true KR830002053B1 (en) 1983-10-08

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US (1) US4299694A (en)
JP (1) JPS5745376A (en)
KR (1) KR830002053B1 (en)
AR (1) AR224456A1 (en)
BR (1) BR8105159A (en)
ES (1) ES503540A0 (en)
GR (1) GR75720B (en)
PT (1) PT73328B (en)
ZA (1) ZA8104421B (en)

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US5411142A (en) * 1993-03-29 1995-05-02 Abbott; Kenneth E. Air-flow control for particle cleaning systems
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US8062410B2 (en) 2004-10-12 2011-11-22 Great River Energy Apparatus and method of enhancing the quality of high-moisture materials and separating and concentrating organic and/or non-organic material contained therein
US8579999B2 (en) 2004-10-12 2013-11-12 Great River Energy Method of enhancing the quality of high-moisture materials using system heat sources
US7275644B2 (en) 2004-10-12 2007-10-02 Great River Energy Apparatus and method of separating and concentrating organic and/or non-organic material
US7540384B2 (en) * 2004-10-12 2009-06-02 Great River Energy Apparatus and method of separating and concentrating organic and/or non-organic material
US7987613B2 (en) 2004-10-12 2011-08-02 Great River Energy Control system for particulate material drying apparatus and process
US8523963B2 (en) 2004-10-12 2013-09-03 Great River Energy Apparatus for heat treatment of particulate materials
US7413084B2 (en) * 2004-10-19 2008-08-19 Wegner Paul C Method and system for separating particulate matter
FR2908673B1 (en) * 2006-11-20 2009-11-06 Fcb Ciment Sa Apparatus for selecting granulometric and / or drying material.
WO2010127036A1 (en) * 2009-04-28 2010-11-04 Mtd America Ltd (Llc) Apparatus and method for separating materials using air
CA2676514A1 (en) * 2009-08-24 2011-02-24 Wood Ash Industries Inc Method for separating biochar from wood ash
CN102716857A (en) * 2012-06-08 2012-10-10 清华大学 Pneumatic particle size classifying device for solid particles
CN104870658B (en) * 2012-10-01 2018-03-16 米德雷克斯技术公司 For improving the apparatus and method for combining furnace charge uniformity in reformation/reduction shaft (tower) furnace
CN106984424A (en) * 2017-02-22 2017-07-28 河北钢铁集团矿业有限公司 A kind of production technology of hyperpure iron extract

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GR75720B (en) 1984-08-02
BR8105159A (en) 1982-04-27
PT73328B (en) 1982-08-19
ES503540D0 (en)
PT73328A (en) 1981-08-01
ZA8104421B (en) 1982-07-28
ES503540A0 (en) 1982-11-16
ES8301119A1 (en) 1982-11-16
JPS5745376A (en) 1982-03-15
US4299694A (en) 1981-11-10
AR224456A1 (en) 1981-11-30
KR830005910A (en) 1983-09-14

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